Catalyst and method for reduction of nitrogen oxides

ABSTRACT

A Selective Catalytic Reduction (SCR) catalyst was prepared by slurry coating ZSM-5 zeolite onto a cordierite monolith, then subliming an iron salt onto the zeolite, calcining the monolith, and then dipping the monolith either into an aqueous solution of manganese nitrate and cerium nitrate and then calcining, or by similar treatment with separate solutions of manganese nitrate and cerium nitrate. The supported catalyst containing iron, manganese, and cerium showed 80 percent conversion at 113 degrees Celsius of a feed gas containing nitrogen oxides having 4 parts NO to one part NO 2 , about one equivalent ammonia, and excess oxygen; conversion improved to 94 percent at 147 degrees Celsius. N 2 O was not detected (detection limit: 0.6 percent N 2 O).

STATEMENT REGARDING FEDERAL RIGHTS

This invention was made with government support under Contract No. W-7405-ENG-36 awarded by the U.S. Department of Energy. The government has certain rights in the invention.

FIELD OF THE INVENTION

The present invention relates generally to the abatement of nitrogen oxides and more particularly to the Selective Catalytic Reduction (SCR) of nitrogen oxides using a zeolite catalyst impregnated with iron, cerium, and manganese.

BACKGROUND OF THE INVENTION

It is generally recognized that nitric oxide (NO), nitrogen dioxide (NO₂), and nitrous oxide (N₂O) are principle contributors to smog and other undesirable environmental effects when they are discharged into the atmosphere. NO_(x) is the term generally used to represent nitric oxide (NO), nitrogen dioxide (NO₂), and nitrous oxide (N₂O), as well as mixtures containing these gases. NO_(x) forms in the high temperature zones of combustion processes. The internal combustion engine, and coal or gas-fired or oil-fired furnaces, boilers and incinerators, all contribute to NO_(x) emissions. Although the concentrations of NO_(x) in the exhaust gases produced by combustion usually are low, the aggregate amount discharged in industrial and/or highly populated areas tends to cause problems. NO_(x) is also produced during a variety of chemical processes such as the manufacture of nitric acid, the nitration of organic chemicals, the production of adipic acid, and the reprocessing of spent nuclear fuel rods.

In general, fuel-rich combustion mixtures produce exhaust gases with less NO_(x) than do lean fuel-air mixtures, i.e. mixtures in which more air is provided than the stoichiometric amount required to completely combust the fuel. Lean fuel mixtures will produce an exhaust gas that contains gaseous oxygen.

The US Environmental Protection Agency is requiring greater levels of NO_(x) abatement from mobile and stationary emission sources. For ‘light duty’ mobile sources such as light trucks and cars, NO_(x) emissions will be required to not exceed 0.07 grams/mile, down from the current level of around 0.8 grams/mile. This represents a NO_(x) abatement requirement of greater than 90% over current technology. Some of this abatement will come from advanced vehicle design and advances in combustion technology, but most of the reduction will come from advanced emission controls of which NO_(x) reduction catalysts are the central technology. Similar reductions will be required of heavy diesel trucks in the near future, hence the need for new technologies having the capability of achieving very high reduction of NO_(x) from lean burn engines, and at low operating temperatures as well (150° C.-250° C.).

Although the NO_(x) gases may be thermodynamically unstable with respect to decomposition into elemental oxygen and nitrogen, no simple, economical method or catalyst has been described for inducing this decomposition at high enough rates over broad temperature ranges to make lean NO_(x) reduction economically feasible. It has been discovered, however, that the addition of a reductant such as ammonia to the exhaust gas, under appropriate conditions, converts NO_(x) to elemental nitrogen and steam.

The process of contacting an industrial flue gas with a catalyst in the presence of ammonia at a temperature usually in the range of about 200 degrees Celsius to about 600 degrees Celsius to reduce NO_(x) in the flue gas is commonly known as the process for Selective Catalytic Reduction (SCR) of NO_(x). Any reference made herein to “Selective Catalytic Reduction,” or to “SCR,” is intended to refer to a process in which a mixture of NO_(x) and NH₃ are induced to react catalytically in the presence of oxygen at elevated temperatures.

For lean burn engine technology to be implemented, catalytic converters must be developed for lean burn engines. The catalyst employed in the converter must be active over a broad range of temperature (usually in the range of about 150-500 degrees Celsius, or broader is better), must have very high activity for the conversion of NO_(x) to elemental nitrogen (N₂) and water (H₂O), must react with a broad range of NO and NO₂ in the gas sent from the engine to the catalytic converter, must be sulfur tolerant, and should not produce N₂O or only a few ppm at most. With these goals in mind, lean burn catalysts that remove NO_(x) from exhaust streams (i.e. deNO_(x) catalysts) are highly sought after and are the focus of considerable research worldwide.

A rather narrow window of satisfactory operating temperatures has characterized most catalysts for lean burn applications. Specifically, they only effectively convert NO_(x) over narrow temperature ranges that do not always match the temperatures at which the NO_(x) is emitted. Some of the better catalyst materials have included metal-substituted zeolite catalysts such as Cu-ZSM-5, Fe-ZSM-5, and related catalysts consisting of various zeolites with metal ions substituted into the zeolite structure. These materials are better in some ways than conventional platinum-based deNO_(x) catalysts, but usually the best operating temperature ranges are too high (above 400 degrees Celcius) and too narrow (only about a hundred degrees Celcius in effective temperature width) for many practical applications. One significant advantage that such ‘base metal’ (non-precious metal) zeolite catalysts have over Pt or other precious metal-containing catalysts (e.g. Pt, Pd, Rh, Ir) is that precious metal containing catalysts are known to produce copious quantities of N₂O in addition to N₂ under lean burn conditions. N₂O emissions are not yet regulated, but because N₂O is a potent greenhouse gas, it is a very undesirable byproduct, and a technologically useful catalyst should produce little, if any N₂O.

It has been recognized that the mechanism of SCR of NO_(x) in the presence of ammonia requires an approximately 1:1 ratio of NO to NO₂ in the feed stream to achieve the highest rates of NO_(x) reduction. Ratios above or below 1 result in significantly slower rates of NO_(x) reduction. As combustion processes generate NO_(x) mixtures having very high NO/NO₂ ratios, i.e. the engine emits mostly NO, a process for reduction of the NO must include a method for oxidizing some of the NO to NO₂; preferably about half of the NO should be converted, resulting in a nearly 1:1 ratio.

Emissions control systems for mobile applications are likely to have an oxidation catalyst upstream from the NO_(x) reduction catalyst to oxidize unburned hydrocarbons. This oxidation catalyst will convert some of the NO to NO₂, perhaps up to 20 to 30 percent at a temperature of about 150 degrees Celsius, but not the 50 percent required to achieve the fastest rates of NO_(x) reduction. Because most NO_(x) catalysts are not capable of oxidizing NO to NO₂ at low temperature, these catalysts cannot assist the hydrocarbon oxidation catalyst to generate the advantageous mixture of NO/NO₂ and so these catalysts are largely ineffective at low temperatures, that being below 300 degrees Celsius where the feed contains mostly NO.

A strategy for improving the low temperature activity of SCR catalysts is to provide an additional non-precious metal containing catalyst that can oxidize NO to NO₂ so that the highest rates of NO_(x) reduction can be realized. This is a strategy employed with the present invention.

In addition, internal combustion engines emit a large amount of unburned hydrocarbons during cold engine start-up. In fact, a large fraction of the total emitted hydrocarbons released during the first minutes of engine operation are due to the uncombusted hydrocarbons. Such release of hydrocarbons after cold engine start-up poses a special problem, as at that point the temperatures of the exhaust gas and the catalytic converter are generally not high enough for conversion of the gaseous pollutants by conventional catalysts. The catalysts in present catalytic converter systems are generally ineffective at ambient temperatures and must reach high temperatures, often in the range of 300 degrees Celcius to 400 degrees Celcius, before they become effective. During this time period, unburned hydrocarbons may adsorb onto the catalyst, causing a further diminution in activity. Indeed, under some circumstances, the adsorbed hydrocarbons may form carbonaceous deposits, requiring high temperatures to remove the deposit oxidatively. This can lead to irreversible damage of the catalyst. Therefore, catalysts that can avoid hydrocarbon deposition at low temperature, or more preferably, oxidize unburned hydrocarbons at the lower temperatures, are highly desired.

SCR processes offer the possibility that unspent ammonia reductant could be emitted to the environment. As ammonia is a regulated toxic substance, there are stringent emissions standards for ammonia. Therefore, another desired feature for a broad temperature range SCR process is one in which very little, if any ammonia is allowed to escape into the atmosphere, even under strenuous transient conditions where the process temperature is increasing rapidly because of load on the engine. In other words, the catalytic NO_(x) reduction process should consume all of the ammonia, or the catalyst should consume any excess ammonia by oxidation. In the latter case, it would be highly advantageous if the oxidation of any excess ammonia did not result in the formation of more NO_(x), but that the oxidation process resulted in the net oxidation of ammonia to N₂—a so-called selective catalytic oxidation process.

A number of zeolite-based catalysts for SCR of NO_(x) with ammonia are described below. Many of these catalysts where their activity is given have been tested in the forms of powders or compacted powders. In these catalytic tests, the flows through the catalyst beds are given in terms of gas hourly space velocity (GHSV). The GHSV is the volume of exhaust passed in one hour divided by the volume of the catalyst bed, and is related to the residence time or reaction time that the gaseous species have to react on the catalyst before they leave the catalyst bed. It is generally desirable to minimize the catalyst volume to the extent possible, and a useful catalyst should have high activity at high GHSV. For combustion processes, the GHSV is typically in a range from about 20,000 h⁻¹ to about 200,000 h⁻¹. One difficulty in comparing the activity of one catalyst to another when relative flow rates are given in terms of GHSV arises when one tries to compare a compacted powder catalyst with a catalyst that is supported on a monolith. In a powder catalyst, the bed volume is measured in a straightforward manner. If the catalyst is supported on a monolith such as a commercial cordierite honeycomb support, then the catalyst volume is given as the volume of the honeycomb. The problem here is that the amount of catalyst supported on the honeycomb is very small; most of the volume of the honeycomb catalyst is void space and the volume of the honeycomb itself. This makes it very difficult to make a simple comparison of catalyst activity between a powder catalyst and a monolith-supported catalyst. A rule of thumb that is commonly used is to make a rough comparison in activity between a powder catalyst and a monolith catalyst is to multiply the GHSV of the powder catalyst by about 4, or conversely to divide the GHSV of the monolith catalyst test result by about 4. For example, if a powder catalyst is reported to have a certain activity at 30,000 h⁻¹ GHSV, then it should be compared to a monolith catalyst at roughly 7,500 h⁻¹ GHSV. Conversely, if a monolith catalyst has been reported to have a certain activity at 30,000 h⁻¹ GHSV, then the powder catalyst should be compared at a GHSV of about 120,000 h⁻¹.

The use of zeolite-based catalysts for the SCR of nitrogen oxides with ammonia is well established. U.S. Pat. No. 4,220,632 to D. R. Pence et al. entitled “Reduction of Nitrogen Oxides With Catalytic Acid Resistant Aluminosilicate Molecular Sieves and Ammonia,” incorporated by reference herein, discloses the catalytic reduction of noxious nitrogen oxides in a waste stream (stack gas from a fossil-fuel-fired power generation plant or other industrial plant off-gas stream) using ammonia as reductant in the presence of a zeolite catalyst in the hydrogen or sodium form having pore openings of about 3 to 10 Angstroms.

U.S. Pat. No. 4,778,665 to Krishnamurthy et al. entitled “Abatement of NO_(x) in Exhaust Gases,” incorporated by reference herein, describes an SCR process for pretreating industrial exhaust gases contaminated with NO_(x) in which the catalyst includes an intermediate pore zeolite with a silica to alumina ratio of at least 50 with a Constraint Index of 1 to 12. These zeolites are sometimes referred to as ZSM-5 type zeolites. The zeolite is preferably in the hydrogen form or has up to about 1 percent of a platinum group metal. According to the '665 patent, the hydrogen form of zeolite ZSM-5 (HZSM-5) catalyzes the SCR reaction at temperatures between about 400 degrees Celsius to about 500 degrees Celsius. At temperatures below about 400 degrees Celsius, HZSM-5 is significantly less efficient at removing nitrogen oxides from the gas stream. These catalysts were tested as compacted powder extrudates at space velocities below 10,000 h⁻¹.

U.S. Pat. No. 5,520,895 to S. B. Sharma et al. entitled “Method for the Reduction of Nitrogen Oxides Using Iron Impregnated Zeolites,” which issued on May 28,1996 and is hereby incorporated by reference, describes a process employing impregnated zeolites as catalysts for the SCR of NO_(x) in exhaust gas. A catalyst used with this process includes an intermediate pore size zeolite powder that has been contacted with a water-soluble iron salt or salt precursor to produce an iron loading of at least 0.4 weight percent, and a binder such as titania, zirconia, or silica. The impregnated zeolite is calcined and hydrothermally treated at a temperature of about 400-850 degrees Celsius to produce a catalyst that is capable of greater than 80 percent conversion of the NO_(x) to innocuous compounds when the catalyst has been aged using 100 percent steam at 700 degrees Celsius for 7 hours prior to sending the exhaust gas over the catalyst. These catalysts were tested as powders at space velocities of 12,000 h⁻¹.

U.S. Pat. No. 6,514,470 to K. C. Ott et al. entitled “Catalysts for Lean Burn Engine Exhaust Abatement,” hereby incorporated by reference, describes the catalytic reduction of nitrogen oxides in an exhaust stream gas using a reductant material and an aluminum-silicate type catalyst having a minor amount of a metal. Nitrogen oxides were reduced in the exhaust stream gas by at least 60 percent at temperatures within the range of from about 200 degrees Celcius to about 400 degrees Celcius. The term “hydrocarbons” as it is used both in the '470 patent and in the present patent application, is meant to refer to hydrocarbons and also to partially oxidized products of hydrocarbons such as oxygenated hydrocarbons (alcohols, ketones, and the like). While hydrocarbons were used as the reductant in the examples disclosed in the '470 patent, it was mentioned that ammonia could also be used. However, no data using ammonia as reductant was presented.

In “A Superior Catalyst for Low-Temperature NO Reduction With NH₃,” Chem. Communications, (2003), pp. 848-849, incorporated by reference herein, Gongshin Qi and Ralph T. Yang report an SCR process using a Mn—Ce mixed-oxide powder catalyst that yields nearly 100 percent NO conversion at 100-150 degrees Celsius at a space velocity of 42,000 h⁻¹ (as a powder), and that SO₂ and water have only slight effects on the activity. The catalyst activity was shown to be dependent on the relative amount of Mn in the catalyst, and also on the calcination temperature used to prepare the catalyst.

In “Low-Temperature SCR of NO With NH₃ over USY-Supported Manganese Oxide-Based Catalysts,” Catalysis Letters, vol. 87, nos. 1-2, Apr. 2003, pp. 67-71, incorporated by reference herein, Gongshin Qi, Ralph T. Yang, and Ramsay Chang report the SCR of NO with ammonia and excess oxygen using manganese oxide, manganese-cerium oxide, and manganese-iron oxide supported on USY (ultrastable (i.e. high Si/Al) Y zeolite). It was found that MnO_(x)/USY had high activity and high selectivity to nitrogen at temperatures of from 80-180 degrees Celsius, and that the addition of iron oxide or cerium oxide increased NO conversion. A catalyst of 14% cerium and 6% manganese impregnated into ultrastable Y zeolite produced nearly 100 percent conversion of NO at 180 degrees Celsius at gas hourly space velocity (GHSV) of 30,000 h⁻¹ as a powder catalyst. The only reported product was N₂ (with no N₂O) below 150 degrees Celsius.

There remains a need for catalysts that show better performance for SCR of NO_(x), especially catalysts that reduce NO_(x) at temperatures less than about 200 degrees Celsius at high space velocities, particularly when supported on monolith honeycomb supports.

Therefore, an object of the present invention is to provide a catalyst for the selective catalytic reduction of NO_(x) in the presence of ammonia that shows excellent conversion at temperatures below 200 degrees Celsius at space velocities greater than 30,000 h⁻¹ when tested as a monolith-supported catalyst, or 120,000 h⁻¹ when tested as a powder.

Additional objects, advantages and novel features of the invention will be set forth in part in the description which follows, and in part will become apparent to those skilled in the art upon examination of the following or may be learned by practice of the invention. The objects and advantages of the invention may be realized and attained by means of the instrumentalities and combinations particularly pointed out in the appended claims.

SUMMARY OF THE INVENTION

In accordance with the purposes of the present invention, as embodied and broadly described herein, the present invention includes a method for the Selective Catalytic Reduction of nitrogen oxides. The method involves contacting an exhaust gas stream that includes nitrogen oxides, ammonia, and oxygen, with a catalyst under conditions effective to catalytically reduce the nitrogen oxides such that less than about 0.6 percent N₂O is generated. The catalyst is a medium pore zeolite that has been ion exchanged with iron to provide an efficient SCR function and impregnated with manganese and cerium to provide an efficient function for the low temperature oxidation of NO to NO₂ and any unburned hydrocarbons. These invention catalysts that combine these dual functions are termed ‘hybrid’ catalysts,’ as they are hybrids of SCR catalysts and potent NO oxidation catalysts.

The invention also includes a supported catalyst effective for the Selective Catalytic Reduction of nitrogen oxides in the presence of ammonia. The catalyst is supported on a monolith, and includes ZSM-5 zeolite that has been exchanged with iron and impregnated with manganese and cerium.

The invention also includes a method for catalytically reducing nitrogen oxides in an exhaust gas stream that contains nitrogen oxides, ammonia, and oxygen. The method involves contacting the exhaust gas stream under conditions effective to catalytically reduce the nitrogen oxides with Fe-ZSM-5 catalyst and thereafter with a second catalyst. The second catalyst includes a medium pore zeolite ion that has been ion exchanged with iron and impregnated with manganese and cerium.

BRIEF DESCRIPTION OF THE DRAWINGS

The accompanying drawings, which are incorporated in and form a part of the specification, illustrate the embodiment(s) of the present invention and, together with the description, serve to explain the principles of the invention. In the drawings:

FIG. 1 shows a graphical representation of percent NO_(x) conversion as a function of temperature at a gas hourly space velocity (GHSV) of 30,000 hr⁻¹ (monolith) and in a temperature range from 100 degrees Celsius to 400 degrees Celsius for the following catalysts and NO_(x) compositions: FeZSM-5/MnOx, 4:1 NO/NO₂ (filled circles); FeZSM-5/CeOx/MnO_(x), 4:1 NO/NO₂ (filled squares); powder catalyst MnO_(x) supported on Y zeolite, 120,000 hr⁻¹ (hollow circles); Ce/MnO_(x) supported on Y zeolite, 4:1 NO/NO₂ (filled diamonds); FeZSM-5, 4:1 NO/NO₂ (filled triangles); and FeZSM-5, 1:1 NO/NO₂ (hollow diamonds).

FIG. 2 shows a graphical representation of % (NO₂/(NO+NO₂)) as a function of temperature in the temperature range of from about 100 degrees Celsius to about 500 degrees Celsius for the following catalysts and conditions: monolith supported FeZSM-5/MnOx, 30,000 hr⁻¹ (hollow circles); invention catalyst monolith-supported FeZSM-5/CeO_(x)/MnO_(y), 30,000 hr⁻¹ (hollow squares); monolith supported Pt, space velocity of 30K (filled diamonds); powder catalyst CeO_(x)/MnO_(x) on Y zeolite, 120,000 hr⁻¹ (filled squares); powder catalyst MnO_(x) supported on Y zeolite 120,000 hr⁻¹ (filled triangles); and powder catalyst MnZSM-5,30K GHSV (x-shaped symbols). The uppermost curve for temperatures up to about 350 degrees Celsius is the equilibrium curve for the oxidation of NO with oxygen to produce NO₂ (hollow circles). FIG. 2 shows that the invention catalysts are superior catalysts for the oxidation of NO to NO₂ at low temperatures, which is a requirement for achieving high rates of NO_(x) conversion by SCR in the presence of ammonia.

FIG. 3 shows a graphical representation of % NO_(x) conversion versus temperature in the temperature range of from about 100 degrees Celsius to about 400 degrees Celsius for the following catalysts and conditions: FeZSM-5(hollow circles); CeOx/FeZSM-5 after the first impregnation with Ce (hollow squares); CeOx/FeZSM-5 after the second impregnation with Ce (filled squares); and MnOx/CeOx/FeZSM-5 (hollow triangles). Cerium impregnation was accomplished by immersing iron zeolite into an aqueous solution of cerous nitrate, followed by drying and calcination to convert the cerous nitrate into cerium oxides (CeO_(x)). As FIG. 3 shows, the measured activity of the catalyst before and after impregnation were not significantly different. However, the addition of MnO_(x) in combination with the cerium oxides improved the performance of the catalyst at lower temperatures (below about 250 degrees Celsius).

FIG. 4 a and FIG. 4 b show graphs related to results of NO_(x) conversion and NO conversion for catalysts A, B, C, D, and E prepared by dip coating a monolith with catalyst solution, drying, and calcination. Catalyst A was prepared by dip-coating a monolith into solutions of 2 molar cerous nitrate and 2 molar manganous nitrate. Catalyst B was prepared by dip-coating a monolith into solutions of 1 molar cerous nitrate and 1 molar manganous nitrate. Catalyst C was prepared by dip-coating a monolith into solutions of 0.5 molar cerous nitrate and 0.5 molar manganous nitrate. Catalyst D was prepared by dip-coating a monolith into solutions of 1 molar manganous nitrate and 0.5 molar cerous nitrate. Catalyst E was prepared by dip-coating a monolith into solutions of 0.5 molar manganous nitrate and 1 molar cerous nitrate. Catalyst A was re-impregnated with the aqueous 2 molar solution of manganese nitrate and cerium nitrate, dried, and calcined to generate Catalyst F. Catalyst F was impregnated again in the cerium and manganese solution, dried, and calcined to generate Catalyst G. The results of NO_(x) conversion and NO conversion for catalyst F and for catalyst G are also shown in FIG. 4 a and FIG. 4 b.

FIG. 5 shows results related to the stability of the Ce, MnO_(x) Fe-ZSM-5/monolith catalyst of the present invention to aging using sulfur trioxide (S0 ₃).

FIG. 6 shows the results of NO_(x) conversion as a function of temperature for a dual bed catalyst of the present invention.

DETAILED DESCRIPTION

The invention relates to the Selective Catalytic Reduction (SCR) of NO_(x) in the presence of ammonia and excess oxygen over a broad temperature range. The invention includes a catalyst that has been shown to convert gaseous mixtures of NO and NO₂ to N₂. The catalyst, an embodiment of which includes a monolith-supported medium pore zeolite ion-exchanged with small amounts of iron, manganese, and cerium, has been demonstrated as being a highly active catalyst for the conversion of NO_(x) in the presence of ammonia in the temperature range from about 200 degrees Celsius to about 400 degrees Celsius, and shows surprising activity at temperatures below 200 degrees Celsius, which is highly desirable because state-of-the-art combustion engines are becoming so efficient that exhaust gas temperatures are dropping into the range below 200 degrees Celsius. Activity at these low temperatures is also desirable because of the emission during ‘cold start’ conditions, which occurs before conventional catalysts become hot enough to display effective catalytic activity.

A standard by which deNO_(x) catalysts are currently being measured is that they perform better than the best commercial catalyst if they can provide better than 60 percent conversion at a temperature of 200 degrees Celsius when 20 percent of the feed into the catalyst is nitrogen dioxide (NO₂). The catalyst of the invention has been shown to meet this standard by displaying greater than 60 percent conversion of a gaseous, 4 to 1 mixture of NO/NO₂ at 200 degrees Celsius.

The exhaust gases that can be treated in the catalytic system of the present invention can come from the combustion of fuels in automotive engines (such as diesel engines), gas turbines, engines using an oxygen-rich mixture (lean-burn conditions), and electrical power generation stations. The term “exhaust gas” means any waste gas that is formed in an industrial process or operation and that is normally disposed of by discharge to the atmosphere, with our without additional treatment. “Exhaust gas” includes the gas produced by internal combustion engines. The composition of such a gas varies and depends on the particular process or operation that leads to its formation. When formed in the combustion of fossil fuels, it will generally include nitrogen, steam and carbon dioxide. In addition it will also contain smaller amounts of NO_(x). The fuels can be, for example, natural gas, gasoline, LPG, kerosene, heavy oil and coal. Fuels that contain sulfur will typically produce an exhaust gas that contains one or more sulfur oxides. Rich fuel-air mixtures will generally produce an exhaust gas that contains little if any free oxygen along with some carbon monoxide, hydrocarbons (where the term ‘hydrocarbons’ is meant to include both hydrocarbons and partially oxidized hydrocarbons, as described earlier), and hydrogen. Lean fuel-air mixtures, which contain more air than what is stoichiometrically required to completely burn the fuel, will form an exhaust gas that contains oxygen. Other industrial processes such as nitration, uranium recovery, and calcining solid salts that contain nitrates produce exhaust gases that can have compositions different from those produced from combustion of fossil fuels. They may be substantially devoid of steam, for example, and may contain very high concentrations of nitrogen or other materials.

The conversion of NO₂ and NO to nitrogen in the presence of ammonia is believed to process generally according to equations (1) and (2) and (3) below. 2 NO₂+4 NH₃+O₂→3 N₂ +6 H ₂O  (1) 4 NO+4 NH₃+O₂→4 N₂+6 H₂O  (2) 2 NO+2 NO₂+4 NH₃→4 N₂+6 H₂O  (3)

The highest rates of NO_(x) conversion by reduction with ammonia occur when the ratio of NO to NO₂ is 1 (equation 3). To achieve the high rate due to the ‘fast’ SCR process of equation 3 from an exhaust stream that contains little NO₂ and mostly NO as the NO_(x) component, sufficient NO must be first oxidized to NO₂ to achieve a ratio of NO to NO₂ that is close to 1.

The present invention is effective for treating exhaust gas containing the approximate stoichiometric amount of ammonia. The ammonia may be present in the gas, may be added to the gas, or may be produced by an upstream process (such as by decomposition of urea). The term “approximate stoichiometric amount” means from about 0.75 to about 1.25 times the molar amount of ammonia indicated in equations (1), (2), and (3) above.

In performance testing of the catalysts and processes of the present invention, a simulated exhaust gas mixture was used. Those skilled in the art will readily recognize that other variations of such simulated exhaust gas mixtures could be employed.

The exhaust gas is typically treated in the catalytic system of this invention at a temperature of from about 50 degrees Celsius to about 1000 degrees Celsius or more, e.g. within the range of within the range of about 100 degrees Celsius to about 900 degrees Celsius, e.g. of about 100 degrees Celsius to about 600 degrees Celsius, e.g. of about 120 degrees Celsius to about 600 degrees Celsius, e.g. of about 120 degrees Celsius to about 400 degrees Celsius, and at a gas hourly space velocity (GHSV, relating to volumes of gas at standard temperature and pressure (STP) per volume of catalyst per hour) adjusted to provide the desired conversion. The GHSV can be from about 1,000 to about 500,000 hr⁻¹, e.g. within the range of about 2,500 to about 250,000 hr⁻¹, e.g. from about 5,000 to about 150,000 hr⁻¹, e.g. from about 10,000 to about 100,000 hr⁻¹.

The process of the invention is operable at subatmospheric to superatmospheric pressure, e.g. from about 5 psia to about 500 psia, preferably from about 10 psia to about 50 psia, i.e. near or slightly above atmospheric pressure.

The gas mixture directed over the catalyst should contain at least a stoichiometric amount of oxygen as indicated by equations (1) and (2), or enough oxygen to convert half the NO to NO₂ to proceed by the way of the ‘fast’ SCR reaction (equation 3). Excess levels of oxygen above the stoichiometric amount may be desirable. According to the method of the invention, a source of oxygen, such as air, is sent to the catalyst along with the exhaust gas. If sufficient oxygen is not present in the exhaust gas, a source of oxygen, e.g. air, may be added to the exhaust gas, and if sufficient oxygen is present in the exhaust gas, then no air need be added to the exhaust gas.

Adequate conversion may be readily achieved with a simple stationary fixed-bed of catalyst. The fixed includes a bed of the invention catalyst, which is a ZSM-5 type zeolite having small amounts of iron, manganese, and cerium impregnated therein. This bed can be used alone, or in combination with other catalyst beds, e.g. a dual bed. A bed of the invention catalyst can be used in combination with another catalyst bed such as a FeZSM-5 catalyst bed, to provide a dual bed that may be capable of even better overall performance than a single bed over the wide range of operating conditions for a combustion engine, for example.

Suitable mixing may be used before the gas reaches the catalyst to produce a homogeneous gas mixture for catalytic conversion. The mixers may be any suitable arrangement, including, for example, baffles, discs, ceramic discs, static mixers, or combinations of these. The mixing may be integral with the gas flow paths.

Catalysts useful with the present invention typically include an active material and a support. Suitable support materials include cordierite, nitrides, carbides, borides, intermetallics, mullite, alumina, natural and synthetic zeolites, lithium aluminosilicate, titania, feldspars, quartz, fused or amorphous silica, clays, aluminates, zirconia, spinels, or metal monoliths of aluminum-containing ferrite type stainless steel, or austenite type stainless steel, and combinations thereof. Typical substrates are disclosed in U.S. Pat. Nos. 4,127,691 and 3,885,977, incorporated by reference herein. The catalyst is combined with the substrate in any method that ensures that the catalyst will remain intact during the catalytic reaction.

A catalyst useful with the present invention comprises a medium pore zeolite, whether naturally occurring or synthesized crystalline zeolites. Preferably these zeolites are medium pore zeolites with a silica to alumina ratio of at least 50. Examples include ZSM-5, ZSM-11, ZSM-12, ZSM-21, ZSM-23, ZSM-35, ZSM-38, and ZSM-48. Preferably, the zeolite is ZSM-5.

An embodiment of the catalyst of the present invention was prepared by ion exchanging a zeolite with iron and then impregnating manganese and cerium onto the iron zeolite in a stepwise fashion. The products were tested at various stages during the preparation. First, a slurry of ZSM-5 was coated onto a monolith of cordierite monolith (the support). The slurry-coated monolith was then dried at a temperature of about 450-500 degrees Celsius. Following the drying, ferric chloride (FeCl₃) was sublimed onto ZSM-5 treated cordierite, after which the product was subjected to calcination at a temperature of about 500 degrees Celsius. This material is abbreviated “FeZSM-5” on FIG. 1 and FIG. 2. The activity of this product was determined by performing Selective Catalytic Reduction (SCR) of NO_(x) using two different gaseous mixtures of nitrogen oxides, 1:1 mixture of NO/NO₂ and a 4:1 mixture of NO/NO₂, in the presence of about 1 equivalent of ammonia and excess oxygen gas. The conversion data for both the 1:1 mixture and the 4:1 mixture are each reported in FIG. 1, which shows a graphical representation of percent NO_(x) conversion as a function of temperature at a GHSV of 30,000 hr⁻¹ and in a temperature range from 100 degrees Celsius to 400 degrees Celsius. The curve with hollow diamond symbols shows the conversion data for the 1:1 mixture, and the curve with triangle symbols shows the conversion data for the 4:1 mixture. As FIG. 1 shows, the material prepared by subliming FeCl₃ onto ZSM-5 converts about 65 percent of the NO_(x) from a feed stream of 4:1 NO/NO₂ at 200 degrees Celcius.

Cerium was added to the iron zeolite catalyst by immersing the catalyst into an aqueous solution of cerous nitrate. The drying and calcining steps converted the cerous nitrate into cerium oxides (CeO_(x)). The activity of this catalyst was measured, and was found not to be significantly different than the starting iron catalyst. The data are plotted on the graph shown in FIG. 3.

The iron- and cerium-containing product catalyst prepared as described above was immersed into an aqueous solution of manganese (II) nitrate, then dried and calcined. The drying and calcinations step are believed to convert at least some of the manganese nitrate into manganese oxides (MnO_(x)) and possibly mixed cerium-manganese oxides. The activity of this catalyst was determined by performing Selective Catalytic Reduction (SCR) with a gas mixture containing a 4:1 mixture of NO/NO₂, about one equivalent ammonia, and excess oxygen gas. The conversion data are shown in FIG. 1 (filled circles). As FIG. 3 shows, the addition of MnO_(x) in combination with the cerium oxides improved the performance of the catalyst by acting as a potent oxidizer, as demonstrated by improved conversion of 4:1 mixture of NO/NO₂ at the lower temperatures.

The performance of the invention catalyst was compared to that of a catalyst powder described by Gonshin Qi et al. in the following paper: “Low-Temperature SCR of NO with NH₃ over USY-supported Manganese Oxide-Based Catalysts,” Catalysis Letters, vol. 87, nos. 1-2. The Qi et al. powder catalyst is composed of 14 percent cerium and 6 percent manganese impregnated into ultrastable (i.e. high Si/Al) Y zeolite, which was reported to promote nearly 100 percent conversion of NO at 180 degrees Celsius under the disclosed experimental conditions. This powder catalyst produced 80 percent conversion when wet at a temperature of 150 degrees Celsius with a feed of 100% NO and a space velocity of 30,000 GHSV. It produced 55 percent conversion at a space velocity of 120,000 GHSV, a temperature of 150 degrees Celsius, and a gas composition of 4:1 NO/NO₂. This is an interesting catalyst and appears to be oxidizing a large fraction of NO to NO₂ to achieve these rates. For NO oxidation at 120,000 GHSV, the results are very similar to that for Platinum. As FIG. 1 and FIG. 2 show, the CeO_(x)/MnO_(x)/Y catalyst of Qi, Yang, and Chang has even better low temperature performance than FeZSM-5. However, as FIG. 1 and FIG. 2 show, the catalyst of the present invention, Ce/MnOx/FeZSM-5 has substantially better low temperature performance.

Another aspect of the present invention relates to “dual bed” catalyst systems. As these new catalysts are too active for ammonia oxidation at high temperature but have fantastic low temperature performance, one solution to get a broader range of operation involves putting a “high temperature catalyst” such as FeZSM-5 that has excellent performance at high temperature in front of a bed of the hybrid catalysts of the invention. At high temperatures, the high temperature catalyst converts NO_(x) to nitrogen with high efficiency. At low temperature, however, the “high temperature” catalyst is capable of only converting around 60 percent of the NO_(x) at 200 degrees Celsius at 4:1 NO/NO₂ feeds. The hybrid catalyst would efficiently convert a large fraction of the remaining NO_(x), likely attaining better than 90 percent conversion over a broad temperature range of about 150 degrees Celsius. This dual functioning catalyst bed enables NO_(x) conversion over broad temperature ranges from 150 degrees Celsius to greater than 450 degrees Celsius, even up to 500 degrees Celsius.

The following EXAMPLES illustrate the operability of the invention.

EXAMPLE 1 Preparation of Fe ZSM-5 Supported on Cordierite Monolith.

Cylinders of cordierite monolith (10 mm in diameter×12 mm long; 400 cells per inch²) were coated with H-ZSM-5 (ZEOLYST INTERNATIONAL) zeolite by dipping the monolith into an aqueous slurry of the zeolite powder followed by drying at 110 degrees Celsius. Several cycles of coating followed by drying were necessary to achieve a zeolite coating of around 20 to 24 percent by weight. The coated monolith was then calcined at a temperature of about 500 degrees Celsius. Iron was exchanged into the pores of the zeolites by the well-known method of gas-phase exchange using FeCl₃ as the volatile iron component. A piece of ZSM-5 coated cordierite monolith was placed into a boat downstream from a boat of anhydrous FeCl₃. The boats were contained within a quartz apparatus that was purged with dry nitrogen gas. The quartz apparatus was heated to a temperature of from between 300 degrees Celsius and 325 degrees Celsius to initiate the sublimation of FeCl₃. After the zeolite-coated monolith had changed to a color of yellow to yellow orange, the apparatus was cooled under dry nitrogen, and the resulting monolith was calcined in ambient air at a temperature of about 500 degrees Celsius to yield a catalyst referred to as Fe-ZSM-5/monolith. The catalyst gained approximately 7 percent by weight of FeO_(x) based on the weight of the zeolite coating.

EXAMPLE 2 Testing of Fe ZSM-5 Monolith Catalyst

The Fe-ZSM-5/monolith prepared according to EXAMPLE 1 was tested for NO_(x) conversion activity and for NO oxidation activity. To measure the activity for NO_(x) conversion, the Fe-ZSM-5/monolith was placed into a 10 mm diameter quartz reactor tube. Reaction gases (NO, NO₂, NH₃, and O₂ in He) were blended using mass flow controllers to produce a gas mixture having 350 parts per million (ppm) total NO_(x), 350 ppm NH₃, and 12 percent O₂; 5 percent steam was added using a syringe pump and an evaporator. The NO:NO₂ ratio was either 1:1 or 4:1. The space velocity was either 30,000 h⁻¹ or 60,000 h⁻¹. Products and reactants (NO, NO₂, N₂O, NH₃) were analyzed using a Fourier Transform Infrared (FT-IR) spectrometer with a heated cell having a 2 meter, or 10 meter, path length. Nitrogen was measured using a gas chromatograph. Operation of the reactor was automated. Catalytic performance data was obtained over the temperature range of 500 degrees Celsius to 120 degrees Celsius. The data is summarized in FIG. 1.

To determine the NO oxidation activity, a blend of 190 ppm NO and 12 percent O₂ in He was fed to the reactor, and the quantity of NO₂ to total NO_(x) was measured using FT-IR. The results of the NO oxidation test are shown in FIG. 2.

EXAMPLE 3 Preparation of MnO_(x)/Y Catalyst

MnO_(x) supported on zeolite Y catalyst comparable to a catalyst reported by Yang et al. (“A Superior Catalyst for Low-Temperature NO Reduction With NH₃,” Chem. Commun. (2003), pp. 848-849) was prepared by incipient wetness impregnation. A six gram sample of zeolite Y (ZEOLYST®) was impregnated with approximately 3 cubic centimeters (cc) of 5 molar manganous nitrate solution to achieve a catalyst having approximately 10 to 15 percent by weight Mn. The catalyst was dried at a temperature of about 120 degrees Celsius, and then calcined at a temperature of about 500 degrees Celsius.

EXAMPLE 4 Testing of MnO_(x)/Y catalyst

The MnO_(x)/Y catalyst prepared in EXAMPLE 3 was tested for NO_(x) conversion in an identical fashion as given in EXAMPLE 2. This catalyst was tested as a powder diluted in 1.5 cc of crushed cordierite. The GHSV of 120,000 h⁻¹ (based on volume of active catalyst powder) was chosen to make a good comparison to other catalytic results from monolith catalysts. The results for the 4:1 NO/NO₂ conditions are shown in FIG. 1. The NO oxidation activity of this catalyst at the same GHSV as the NO_(x) conversion experiment and as a function of temperature was determined as described in EXAMPLE 2. The data are presented in FIG. 2.

EXAMPLE 5 Preparation and Testing of MnO_(x)/Y Catalyst

A Ce,MnO_(x) supported on zeolite Y catalyst comparable to the catalyst reported by Yang et al (“A Superior Catalyst for Low-Temperature NO Reduction With NH₃,” Chem. Commun. (2003), pp. 848-849) was prepared by incipient wetness impregnation of a powdered sample of zeolite Y with an aqueous solution of Ce and Mn nitrates to achieve a 6% Mn, 14% Ce by weight catalyst. After the incipient wetness impregnation was performed, the catalyst was dried overnight at a temperature of about 120 degrees Celsius, and then calcined at a temperature of about 500 degrees Celsius. The product Ce,MnO_(x)N/Y catalyst was tested for NO_(x) conversion as described in EXAMPLE 2. Ce,MnO_(x)/Y catalyst powder was diluted 50/50 with 1.5 cc of crushed cordierite. The GHSV of 120,000 h⁻¹ (based on volume of active catalyst powder) was chosen to make a good comparison to other catalytic results from monolith catalysts. The results for the 4:1 NO/NO₂ conditions are shown in FIG. 1.

The NO oxidation activity of this catalyst at the same GHSV as the NO_(x) conversion experiment and as a function of temperature was determined as described in EXAMPLE 2. The data is presented in FIG. 2.

EXAMPLE 6 Preparation of CeO_(x)-Fe-ZSM-5/Monolith Catalyst

The Fe-ZSM-5/monolith catalyst from EXAMPLE 1 was dip coated in an aqueous 4M cerous nitrate solution. The excess solution was shaken off, and the catalyst dried at a temperature of about 120 degrees Celsius. The catalyst was then calcined at a temperature of about 500 degrees Celsius. The product was CeO_(x)-Fe-ZSM-5/monolith catalyst.

EXAMPLE 7 Testing of CeO_(x)-Fe-ZSM-5/Monolith Catalyst

The CeO_(x)-Fe-ZSM-5/monolith catalyst was tested for NO_(x) conversion in an identical fashion as described in EXAMPLE 2. CeO_(x)-Fe-ZSM-5/monolith catalyst powder was diluted 50/50 with 1.5 cc of crushed cordierite. The GHSV of 120,000 h⁻¹ was chosen to make a good comparison to other catalytic results from monolith catalysts. The results for the 4:1 NO/NO₂ conditions are shown in FIG. 3.

EXAMPLE 8 Preparation of CeO_(x)-Fe-ZSM-5/Monolith Catalyst

The CeO_(x)-Fe-ZSM-5/monolith catalyst from EXAMPLE 6 was impregnated a second time by dip coating in an aqueous solution of 4M cerous nitrate. The catalyst was dried and calcined as described in EXAMPLE 6.

EXAMPLE 9 Testing of CeO_(x)-Fe-ZSM-5/Monolith Catalyst

The CeO_(x)-Fe-ZSM-5/monolith catalyst of EXAMPLE 8 (having the additional impregnation/calcination treatment) was tested for NO_(x) conversion using the identical conditions as in EXAMPLE 2. The test result data showed little difference from the data for the catalyst given in EXAMPLE 7. The data are plotted in FIG. 3.

EXAMPLE 10 Preparation of Mn,CeO_(x)-Fe-ZSM-5 Monolith Catalyst

The CeO_(x)-Fe-ZSM-5/monolith catalyst from EXAMPLE 7 was impregnated with Mn by dip coating the monolith into an aqueous solution of 1 molar manganous nitrate. The excess solution was shaken off and the catalyst was then dried at a temperature of about 120 degrees Celsius and afterward calcined at a temperature of about 500 degrees Celsius. The product was the catalyst Mn,CeO_(x)-Fe-ZSM-5.

EXAMPLE 11 Testing of Mn,CeO_(x)-Fe-ZSM-5 Monolith Catalyst

The Mn,CeO_(x)-Fe-ZSM-5/monolith catalyst prepared as described in EXAMPLE 10 was tested for NO_(x) conversion using the same conditions as in EXAMPLE 2. These data are shown in FIG. 1.

The NO oxidation capability of this catalyst was tested using 190 ppm NO as described in EXAMPLE 2. The data are shown in FIG. 3.

EXAMPLE 12 Preparation of Five Mn,CeO₂-Fe-ZSM-5 Monolith Catalysts

A series of catalysts were prepared to examine the relationship of the amount of Ce and Mn and the effect on catalytic activity for NO_(x) conversion and NO oxidation. Five pieces of cordierite monolith (10 mm diameter, 12 mm long, 400 cells per inch) were coated with an aqueous slurry of NH₄ ⁺-ZSM-5. The average zeolite loading was 34 percent by weight. The catalysts were dried, calcined, and treated with FeCl₃ as in EXAMPLE 1. These five identically prepared Fe-ZSM-5/monolith catalysts were then impregnated with varying amounts of Ce and Mn by dip-coating them into aqueous solutions of cerium nitrate and manganese nitrate as follows:

-   -   Catalyst A was prepared by dip-coating a monolith into solutions         of 2 molar cerous nitrate and 2 molar manganous nitrate.     -   Catalyst B was prepared by dip-coating a monolith into solutions         of 1 molar cerous nitrate and 1 molar manganous nitrate.     -   Catalyst C was prepared by dip-coating a monolith into solutions         of 0.5 molar cerous nitrate and 0.5 molar manganous nitrate.     -   Catalyst D was prepared by dip-coating a monolith into solutions         of 1 molar manganous nitrate and 0.5 molar cerous nitrate.     -   Catalyst E was prepared by dip-coating a monolith into solutions         of 0.5 molar manganous nitrate and 1 molar cerous nitrate.

After dip-coating each monolith, the excess solution was removed from each of the monolith pieces, and all five pieces of catalyst were dried and calcined as described before.

EXAMPLE 13 Testing of Five Mn,CeO_(x)-Fe-ZSM-5 Monolith Catalysts

The catalysts A-E from EXAMPLE 12 were tested for NO_(x) conversion and NO oxidation using the method given in EXAMPLE 2. The results of NO_(x) conversion and NO conversion are given in FIG. 4 a and FIG. 4 b.

EXAMPLE 14 Preparation of Two Mn,CeO_(x)-Fe-ZSM-5 Monolith Catalysts

Catalyst A from EXAMPLE 12 was re-impregnated with the aqueous 2 molar solution of manganese nitrate and cerium nitrate, dried, and calcined to generate Catalyst F. The NO_(x) conversion and NO conversion for catalyst F were measured. Afterward, catalyst F was impregnated again in the cerium and manganese solution, dried, and calcined to generate Catalyst G. The results of NO_(x) conversion and NO conversion for catalyst F and for catalyst G are shown in FIG. 4 a and FIG. 4 b.

EXAMPLE 15 Oxidation of Ammonia Using Mn,CeO_(x)-Fe-ZSM-5 Monolith Catalyst

Catalyst F was used to demonstrate the capability of using Mn,CeO_(x)-Fe-ZSM-5 monolith catalyst to oxidize ammonia and thereby minimize the loss of any excess or unconsumed ammonia (sometimes known as the ammonia ‘slip’) into the environment. Catalyst F was placed into a 10 mm diameter quartz reactor. A gas mixture including about 500 ppm of NH₃ and 12 percent O₂ diluted in He were delivered to the reactor along with 5 percent steam. The conversion of ammonia was monitored by FT-IR and gas chromatography (GC) to detect N₂. At a temperature of about 300 degrees Celsius, the ammonia was completely converted. The selectivity to N₂ was about 80 percent, and the selectivity to NO_(x) was about 20 percent.

EXAMPLE 16 Resistance of Mn, CeO_(x)-Fe-ZSM-5 Monolith Catalyst to Hydrocarbon Poisoning

Catalyst F was used to demonstrate the resistance of Mn,CeO_(x)-Fe-ZSM-5 monolith catalyst to hydrocarbon poisoning. While maintaining the catalyst at a temperature of 177 degrees Celsius, a NO/NO₂ ratio of 4:1, and the conditions given in EXAMPLE 2, the NO_(x) conversion of 95 percent was measured. A train of 4 pulses of 10 microliters of liquid toluene injected at 4 minute intervals were then vaporized and delivered upstream of the catalyst bed. After each pulse, a sharp decrement in NO_(x) conversion was noted, declining by about 10 points, but then rapidly recovering to above 90 percent. After the 4 pulses of toluene, NO_(x) conversion was greater than 90 percent, and recovered to 95 percent conversion in less than 3 hours.

EXAMPLE 17 Stability of Ce, MnO_(x) Fe-ZSM-5/Monolith Catalyst to Aging with SO₃

The Ce, MnO_(x) Fe-ZSM-5/monolith catalyst from EXAMPLE 10 was tested for stability to SO₃ aging. A blend of 45 ppm SO_(x), mostly SO₃, in air with steam was passed over the catalyst for 15 hours while the temperature of the catalyst was held at a temperature of about 350 degrees Celsius. The catalyst was then heated briefly to a temperature of about 500 degrees Celsius, and the NO_(x) conversion in a 4:1 NO/NO₂ blend was tested as outlined in EXAMPLE 2. The data are shown graphically in the plot shown in FIG. 5. The shape of the curve for NO_(x) conversion changed, but NO_(x) conversion remained greater than 80 percent at a temperature of about 200 degrees Celsius, and was greater than 90 percent from a temperature of about 275 degrees Celsius to a temperature of about 475 degrees Celsius.

EXAMPLE 18 Dual Bed Catalyst

To provide a broad temperature window process, dual bed catalysts were prepared. Catalyst F from EXAMPLES 14, 15, and 16 was placed downstream from a 10 mm diameter×12 mm long piece of Fe-ZSM-5/monolith catalyst prepared as described in EXAMPLE 1. The dual bed catalyst was tested as described in EXAMPLE 2, except that the flow was doubled to account for the doubling of volume of the overall bed; thus the GHSV for the dual bed was 30,000 h⁻¹. The NO_(x) conversion as a function of temperature is shown in FIG. 6.

EXAMPLE 19 Dual Bed Catalyst

A dual bed catalyst was prepared by placing a 10 mm diameter×5.4 mm diameter piece of Fe-ZSM-5 monolith catalyst prepared as in EXAMPLE 1 upstream from catalyst F (from EXAMPLE 18). The flow rate was adjusted to give an overall GHSV of 30,000 h⁻¹. The results of the NO_(x) conversion test are shown in FIG. 6.

EXAMPLE 20 Stability of Dual Bed Catalyst to Hydrocarbon Poisoning

The dual bed catalyst from EXAMPLE 19 was subjected to the standard 4:1 NO/NO₂ ratio NO_(x) conversion conditions at a temperature of 160° C. NO_(x) conversion was constant at 85% prior to introduction of toluene. Toluene vapor was introduced at a concentration of 100 ppm. During the next 2 hours, the conversion of NO_(x) did not change. The concentration of toluene was then increased to 1000 ppm. Over the next two hours, the NO_(x) conversion slowly dropped to about 65 percent. Upon heating the catalyst bed to a temperature of about 250 degrees Celsius with 1000 ppm toluene still in the feed, NO_(x) conversion rose to about 85 percent and was steady. All catalytic activity was regained when toluene was removed from the feed and the catalyst bed was heated briefly to a temperature of 250-300° C.

The foregoing description of the invention has been presented for purposes of illustration and description and is not intended to be exhaustive or to limit the invention to the precise form disclosed, and obviously many modifications and variations are possible in light of the above teaching. For example, it is believed that while iron was incorporated into the zeolite structure by sublimation, iron may also be incorporated by ion exchange techniques as well.

The embodiment(s) were chosen and described in order to best explain the principles of the invention and its practical application to thereby enable others skilled in the art to best utilize the invention in various embodiments and with various modifications as are suited to the particular use contemplated. It is intended that the scope of the invention be defined by the claims appended hereto. 

1. A method for the Selective Catalytic Reduction of nitrogen oxides in an exhaust gas stream comprising nitrogen oxides, ammonia, and oxygen, comprising contacting the exhaust gas stream with a catalyst under conditions effective to catalytically reduce the nitrogen oxides such that no more than 0.6 percent N₂O remains, the catalyst comprising a medium pore zeolite, the zeolite being ion exchanged with iron and impregnated with manganese and cerium.
 2. The method of claim 1, wherein the catalyst is characterized as having sufficient catalytic activity to reduce the nitrogen oxides in a gas mixture comprising about 4 parts NO to about 1 part NO₂ by about 80 percent at a temperature of about 113 degrees Celsius, and by about 94 percent at a temperature of about 147 degrees Celsius.
 3. The method of claim 1, wherein the medium pore zeolite is selected from the group consisting of ZSM-5, ZSM-11, ZSM-12, ZSM-21, ZSM-22, ZSM-23, ZSM-35, ZSM-38, ZSM-48, ZSM-57, and ZSM-58.
 4. The method of claim 1, wherein the medium pore zeolite comprises ZSM-5.
 5. The method of claim 1, wherein the medium pore zeolite is supported on a monolith.
 6. The method of claim 1, wherein the medium pore zeolite is supported on cordierite.
 7. A supported catalyst effective for the Selective Catalytic Reduction of nitrogen oxides in the presence of ammonia comprising a catalyst supported on a monolith, said catalyst comprising ZSM-5 ion exchanged with iron and impregnated with manganese and cerium.
 8. The supported catalyst of claim 7, wherein said monolith comprises cordierite.
 9. A method for catalytically reducing nitrogen oxides in an exhaust gas stream containing nitrogen oxides, ammonia, and oxygen comprising contacting the exhaust gas stream under conditions effective to catalytically reduce the nitrogen oxides with a first catalyst comprising Fe-ZSM-5 and thereafter with a second catalyst comprising a medium pore zeolite ion exchanged with iron and impregnated with manganese and cerium.
 10. The method of claim 9, wherein the second catalyst is characterized as having sufficient catalytic activity so as to reduce the nitrogen oxides in a 4 to 1 mixture of NO to NO₂, respectively, by about 80 percent at a temperature of about 113 degrees Celsius, and by about 94 percent at a temperature of about 147 degrees Celsius when the exhaust gas comprises oxygen and nitrogen oxides comprising NO and NO₂ in a ratio of about 4 to
 1. 11. The method of claim 9, wherein the medium pore zeolite is selected from the group consisting of ZSM-5, ZSM-11, ZSM-12, ZSM-21, ZSM-22, ZSM-23, ZSM-35, ZSM-38, ZSM-48, ZSM-57, and ZSM-58.
 12. The method of claim 9, wherein the medium pore zeolite comprises ZSM-5.
 13. The method of claim 9, wherein the Fe-ZSM-5 and the second catalyst are supported on a monolith.
 14. A catalyst effective for the selective catalytic reduction of nitrogen oxides prepared by ion exchanging a medium pore zeolite with iron impregnating the zeolite with cerium and manganese, wherein ion exchanging is followed by calcination at a temperature of from about 450 degrees Celsius to about 500 degrees Celsius, wherein impregnation with cerium comprises exposure to an aqueous solution comprising cerium followed by drying and calcination; and wherein impregnation with manganese comprises exposure to an aqueous solution of manganese (II) followed by drying and calcination.
 15. The method according to claim 14, wherein the medium pore zeolite is selected from the group consisting of ZSM-5, ZSM-11, ZSM-12, ZSM-21, ZSM-22, ZSM-23, ZSM-35, ZSM-38, ZSM-48, ZSM-57, and ZSM-58.
 16. The method according to claim 14, wherein the medium pore size zeolite comprises ZSM-5.
 17. A dual bed catalyst system comprising a first catalyst portion that includes Fe-ZSM-5 and a second catalyst portion that includes a medium pore zeolite ion exchanged with iron and impregnated with manganese and cerium. 